EP0610168B1 - Verfahren zur Herstellung von Benzin mit hoher Oktanzahl - Google Patents
Verfahren zur Herstellung von Benzin mit hoher Oktanzahl Download PDFInfo
- Publication number
- EP0610168B1 EP0610168B1 EP94870015A EP94870015A EP0610168B1 EP 0610168 B1 EP0610168 B1 EP 0610168B1 EP 94870015 A EP94870015 A EP 94870015A EP 94870015 A EP94870015 A EP 94870015A EP 0610168 B1 EP0610168 B1 EP 0610168B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- stage
- transalkylation
- fraction
- reforming
- heavy
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 238000000034 method Methods 0.000 title claims abstract description 24
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 title claims abstract description 9
- 238000010555 transalkylation reaction Methods 0.000 claims abstract description 23
- 238000002407 reforming Methods 0.000 claims abstract description 19
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 39
- 239000003054 catalyst Substances 0.000 claims description 19
- 239000000203 mixture Substances 0.000 claims description 11
- 238000001833 catalytic reforming Methods 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 229910052680 mordenite Inorganic materials 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 claims 2
- 239000000446 fuel Substances 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000009835 boiling Methods 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 239000000686 essence Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- -1 compounds metals Chemical class 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000008707 rearrangement Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910052702 rhenium Inorganic materials 0.000 description 1
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G63/00—Treatment of naphtha by at least one reforming process and at least one other conversion process
- C10G63/02—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G59/00—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha
- C10G59/02—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha plural serial stages only
Definitions
- the present invention relates to a method for improving the yield of high octane number gasolines.
- the present invention is relates to a process for increasing the yield of high index species octane during the naphtha reforming step.
- Naphtha is a fraction that has its temperature boiling range between 80 and 200 ° C and which consists essentially of paraffins, naphthenes and aromatics.
- the most important reaction that takes place during naphtha reforming consists of the dehydrocyclization of paraffins in aromatics.
- catalytic reforming has tendency to increase the end point of the reformate with respect to naphtha and promote the formation of benzene.
- these phenomena are all the more marked.
- those skilled in the art know that the endpoint of the reformate must be sufficiently low and that the content of benzene should be limited
- the object of the present invention is a method which makes it possible to increase the gasoline yield with high octane number, namely the fraction intermediate from the naphtha reforming step.
- FIG. 1 represents a schematic diagram of the method of the invention.
- a charge of naphtha is subject to a reforming step (2) during which is brought into contact with a reforming catalyst in appropriate conditions.
- the effluent recovered from the reforming step by the line (21) is introduced into the separation stage (3) and separated into three fractions: the light fraction (31), rich in benzene, and whose boiling point is generally less than 90 ° C, the fraction intermediate (32) whose boiling point is generally understood between 90 and 180 ° C and the heavy fraction (33) whose temperature boiling point is generally above 180 ° C.
- the heavy and light fractions are then mixed and introduced into a transalkylation reactor (4) in which it is brought into contact with a transalkylation catalyst under suitable conditions.
- This transalkylation step can be carried out in ascending or descending mode.
- the effluent from this transalkylation step is sent via line (41) to line (21) where it is mixed with the effluent from catalytic reforming.
- the whole is sent to the separation step at the end of which a larger intermediate fraction is recovered.
- the pipes (311) and (331) indicated in FIG. 1 are not used.
- Catalytic reforming of hydrocarbons is well known to those skilled in the art.
- the objective of catalytic reforming is the selective conversion of saturated hydrocarbons to aromatics. This process makes it possible to obtain gasolines with high octane number as well as aromatic hydrocarbons. Many reactions take place during catalytic reforming, the main one being dehydrogenation.
- the catalysts generally used have a double function: a metallic element makes it possible to catalyze dehydrogenation / hydrogenation and an acid function catalyzes the rearrangements of hydrocarbons.
- These catalysts usually contain a small amount of highly dispersed platinum (preferably less than 1% by weight) supported on alumina with a high specific surface (of the order of 150-300m 2 / g); a second metal such as rhenium is also often used. It also happens that the catalyst used is dispersed on a basic support.
- the operating conditions used are generally a temperature between 400 and 550 ° C and a pressure between 0.3 and 3.5 MPa.
- the reaction is generally carried out in reactors with fixed or moving beds.
- U.S. Patent 3,927,136 submits a mixture of a light fraction and a portion of heavy fractions at a transalkylation stage.
- the Applicant unexpectedly found that by submitting the mixing of the heavy and light fractions in a transalkylation stage and in reintroducing the effluent resulting in the separation step, we increased the total amount of intermediate fraction i.e. the yield of gasoline with high octane number.
- step c step of mixture of the light fraction and the heavy fraction
- any other source diluted benzene and / or any other source of polyalkylbenzene it is also possible to introduce in step c (step of mixture of the light fraction and the heavy fraction) any other source diluted benzene and / or any other source of polyalkylbenzene.
- This patent describes a process for transalkylating a charge containing at least one polyalkylbenzene in a reactor in the presence of a catalyst transalkylation to produce at least one characterized monoalkylbenzene in that the reaction is carried out in the presence of hydrogen.
- transalkylation catalysts all kinds.
- these are the molecular sieve catalysts doped with hydrogenation compounds metals based on group VIII metals of the periodic table elements, such as, in particular, nickel, palladium and platinum.
- Large pore molecular sieves will be particularly suitable; we preferably use those with a stress index less than 1.
- the definition of the stress index and its calculation are given in column 5 of US Patent 4,211,886.
- mordenite type catalysts in particular type catalysts Mordenite slightly deficient in aluminum and having a molar ratio silica / alumina up to 30, preferably up to 20.
- mordenite catalysts which can be used according to the present invention, mention may also be made of those described in the US patents 4,665,258 and US 4,723,048.
- One of the advantages brought about by the process of the present invention consists in the recovery of the heavy fraction from the reforming step.
- Another advantage of the process of the present invention consists in that that it allows to treat loads of naphtha without treatment prior to reforming. Indeed, it is known to those skilled in the art that in order to minimize the amount of heavy fraction after reforming, it is preferable to treat the starting naphtha charge by removing the compounds with high boiling temperatures. According to the process of the present invention this naphtha pre-treatment step is no longer necessary which represents a considerable advantage.
- the light fraction obtained is rich in benzene.
- this light fraction was incorporated into essences which often required treatment in order to limit the benzene content of gasolines. This additional step is no longer necessary according to the process of the present invention because the content of benzene is automatically limited following the conversion of benzene during of the transalkylation step.
- the catalyst used is based on nickel (1.6% by weight) deposited on a mordenite with a silica / alumina molar ratio of 8.8.
- This catalyst was activated in the following way: under 6 MPa, with a flow of hydrogen, the temperature gradually rose to 200 ° C and maintained 12 hours. Then, the temperature rose to 360 ° C and stabilized for 4 hours. Then, the reactor is cooled to 200 ° C.
- the operating conditions of the transalkylation are indicated in Table 2.
- the composition of the transalkylation effluent is also indicated in Table 2.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Claims (5)
- Verfahren zum Erhöhen der Ausbeute von Kraftstoffen mit hohem Octanindex, welches die Stufen umfaßt, die bestehen ausa. Aussetzen einer Naphthaladung einem katalytischen Reforming durch in Kontakt bringen mit einem Katalysator von katalytischem Reforming zum Bilden von drei Fraktionen, einer leichten, einer intermediären und einer schweren,b. Trennen der drei Fraktionen während einer Trennungsstufe,c. Mischen von mindestens einem Teil der leichten Fraktion mit mindestens einem Teil der schweren Fraktion,d. Aussetzen der Mischung, abstammend von Punkt c, einer Transalkylierungsstufe unde. Einführen des Ausflusses in die Stufe b, der aus der Stufe d stammt, und Gewinnen einer wichtigeren intermediären Fraktion nach dieser Stufe b, dadurch gekennzeichnet, daß der aus der Reformingstufe gewonnene Ausfluß direkt in die Trennungsstufe eingeführt wird, und dadurch, daß die Gesamtheit der leichten Fraktion und der schweren Fraktion in die Stufe d eingeführt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Transalkylierungsstufe sich in Gegenwart von Wasserstoff abspielt.
- Verfahren nach einem der Ansprüche 1 und 2, dadurch gekennzeichnet, daß eine Quelle unterschiedlich von Benzol und/oder von Polyalkylbenzol in Stufe c hinzugegeben wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß sich die Transalkylierungsstufe in Gegenwart eines Transalkylierungskatalysators abspielt, ausgewählt unter den Molekülsieben mit großen Poren mit einem Spannungsindex unterhalb von 1.
- Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß der Transalkylierungskatalysator ein Mordenit ist.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BE9300104A BE1006675A3 (fr) | 1993-02-02 | 1993-02-02 | Procede de production d'essences a haut indice d'octane. |
BE9300104 | 1993-02-02 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0610168A1 EP0610168A1 (de) | 1994-08-10 |
EP0610168B1 true EP0610168B1 (de) | 1999-04-07 |
Family
ID=3886829
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP94870015A Expired - Lifetime EP0610168B1 (de) | 1993-02-02 | 1994-01-31 | Verfahren zur Herstellung von Benzin mit hoher Oktanzahl |
Country Status (9)
Country | Link |
---|---|
US (1) | US6281398B1 (de) |
EP (1) | EP0610168B1 (de) |
JP (1) | JP3469625B2 (de) |
AT (1) | ATE178647T1 (de) |
BE (1) | BE1006675A3 (de) |
DE (1) | DE69417607T2 (de) |
DK (1) | DK0610168T3 (de) |
ES (1) | ES2131660T3 (de) |
GR (1) | GR3030656T3 (de) |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5347061A (en) * | 1993-03-08 | 1994-09-13 | Mobil Oil Corporation | Process for producing gasoline having lower benzene content and distillation end point |
US7708956B2 (en) * | 2007-09-07 | 2010-05-04 | Uop Llc | Combination hot separator and reactor vessel for simultaneously desulfurizing two vapor streams |
WO2013166235A2 (en) | 2012-05-02 | 2013-11-07 | Saudi Arabian Oil Company | Maximizing aromatics production from hydrocracked naphtha |
FR3014895B1 (fr) * | 2013-12-17 | 2017-02-10 | Ifp Energies Now | Procede de reformage catalytique |
FR3014894B1 (fr) * | 2013-12-17 | 2017-02-10 | Ifp Energies Now | Procede de reformage catalytique |
ES2735104T3 (es) * | 2014-07-07 | 2019-12-16 | Albemarle Europe Sprl | Proceso de alquilación que usa un catalizador que comprende zeolitas que contienen tierras raras ricas en cerio y un metal de hidrogenación |
US10633596B2 (en) * | 2016-06-17 | 2020-04-28 | Basf Corporation | FCC catalyst having alumina derived from crystalline boehmite |
US10093873B2 (en) | 2016-09-06 | 2018-10-09 | Saudi Arabian Oil Company | Process to recover gasoline and diesel from aromatic complex bottoms |
US11066344B2 (en) | 2017-02-16 | 2021-07-20 | Saudi Arabian Oil Company | Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock |
KR102529299B1 (ko) * | 2017-03-01 | 2023-05-08 | 알베마를 유럽 에스알엘 | 개선된 옥탄가를 갖는 알킬화 방법 |
FR3068967B1 (fr) * | 2017-07-13 | 2019-06-28 | IFP Energies Nouvelles | Methode et procede pour convertir l'ethylene present dans l'effluent de tete d'un fcc de maniere a augmenter la production de propylene |
US11613714B2 (en) | 2021-01-13 | 2023-03-28 | Saudi Arabian Oil Company | Conversion of aromatic complex bottoms to useful products in an integrated refinery process |
US11591526B1 (en) | 2022-01-31 | 2023-02-28 | Saudi Arabian Oil Company | Methods of operating fluid catalytic cracking processes to increase coke production |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3927136A (en) * | 1974-07-05 | 1975-12-16 | Texaco Inc | Treatment of hydrocarbons |
US4078990A (en) * | 1977-03-04 | 1978-03-14 | Mobil Oil Corporation | Manufacture of lower aromatic compounds |
US4211886A (en) * | 1978-09-25 | 1980-07-08 | Mobil Oil Corporation | Manufacture of benzene, toluene and xylene |
JPH03501975A (ja) | 1988-06-23 | 1991-05-09 | エービービー ルーマス クレスト インコーポレーテッド | 改良されたポリアルキルベンゼンのアルキル交換反応法 |
IT1236511B (it) * | 1989-10-06 | 1993-03-11 | Eniricerche Spa | Metodo per il recupero di trimetilbenzeni da miscele che li contengono. |
US5053573A (en) * | 1990-09-14 | 1991-10-01 | Mobil Oil Corporation | Reduction of benzene content of reformate by reaction with cycle oils |
-
1993
- 1993-02-02 BE BE9300104A patent/BE1006675A3/fr not_active IP Right Cessation
-
1994
- 1994-01-31 ES ES94870015T patent/ES2131660T3/es not_active Expired - Lifetime
- 1994-01-31 AT AT94870015T patent/ATE178647T1/de not_active IP Right Cessation
- 1994-01-31 DE DE69417607T patent/DE69417607T2/de not_active Expired - Lifetime
- 1994-01-31 DK DK94870015T patent/DK0610168T3/da active
- 1994-01-31 EP EP94870015A patent/EP0610168B1/de not_active Expired - Lifetime
- 1994-02-01 JP JP02760294A patent/JP3469625B2/ja not_active Expired - Fee Related
-
1999
- 1999-06-30 GR GR990401742T patent/GR3030656T3/el unknown
- 1999-10-28 US US09/429,678 patent/US6281398B1/en not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
ATE178647T1 (de) | 1999-04-15 |
ES2131660T3 (es) | 1999-08-01 |
DE69417607T2 (de) | 1999-10-14 |
DK0610168T3 (da) | 1999-10-18 |
US6281398B1 (en) | 2001-08-28 |
GR3030656T3 (en) | 1999-10-29 |
EP0610168A1 (de) | 1994-08-10 |
BE1006675A3 (fr) | 1994-11-16 |
JPH06271871A (ja) | 1994-09-27 |
DE69417607D1 (de) | 1999-05-12 |
JP3469625B2 (ja) | 2003-11-25 |
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